KR20020072360A - Biological Nitrogen Removal from Nitrogen-Rich Wastewaters by Partial Nitrification and Anaerobic Ammonium Oxidation - Google Patents
Biological Nitrogen Removal from Nitrogen-Rich Wastewaters by Partial Nitrification and Anaerobic Ammonium Oxidation Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1263—Sequencing batch reactors [SBR]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/282—Anaerobic digestion processes using anaerobic sequencing batch reactors
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/10—Temperature conditions for biological treatment
Abstract
Description
본 발명은 간헐포기 SBR공정에서 암모니아성 질소(NH4 +-N)를 아질산성 질소(NO2 --N)로 산화시키기 위한 생물학적 단위공정과 연속식 여상 반응조(SMR)의 유입수를 무산소상태로 공급하기 위한 탈산소조, 혐기성 암모니아 산화반응을 유도하기 위한 연속식 여상 반응조(SMR)를 이용한 고농도 질소폐수의 처리장치와 이것을 이용한 수처리방법에 관한 것이다.In the present invention, the biological unit process for oxidizing ammonia nitrogen (NH 4 + -N) to nitrite nitrogen (NO 2 -- N) in the intermittent aeration SBR process and the influent of the continuous filter reactor (SMR) in an anoxic state The present invention relates to a treatment apparatus for high concentration nitrogen wastewater using a deoxygenation tank for supply and a continuous filter reactor (SMR) for inducing anaerobic ammonia oxidation and a water treatment method using the same.
종래의 질소폐수 처리방법은 고농도로 유입되는 질소폐수를 적절히 처리하는 데 어려움이 많고 이러한 폐수를 처리하기 위하여 제안된 종래의 여러 가지 방법은 탈질과정에서 추가적인 외부 탄소원의 주입이 필수적이었다.Conventional nitrogen wastewater treatment methods are difficult to properly treat the nitrogen wastewater flowing into high concentrations, and the various conventional methods proposed for treating such wastewater have been necessary to inject additional external carbon sources in the denitrification process.
본 발명의 목적은 하천의 부영양화의 주범인 고농도 질소폐수를 유효적절하게 처리하기 위한 것이다.It is an object of the present invention to effectively treat high concentrations of nitrogen wastewater, which are the main culprit of eutrophication of rivers.
상기한 종래의 고농도 질소폐수를 처리하는 방법이 안고있는 문제점들을 해결하기 위한 방법으로 적합한 본 발명은 간헐포기 SBR 반응조와 탈산소조 및 연속식 여상 반응조(SMR)를 이용하여 부분아질산화와 혐기성 암모니아 산화반응을 일으킴으로써 외부 탄소원의 공급 없이 고농도 질소폐수를 효과적으로 처리하는 것을 특징으로 한다.The present invention is suitable as a method for solving the problems of the conventional method for treating high concentration nitrogen wastewater. Partial nitrification and anaerobic ammonia oxidation using an intermittent aeration SBR reactor and a deoxygenation tank and a continuous filter reactor (SMR) The reaction is characterized by the effective treatment of high concentration nitrogen wastewater without supply of external carbon source.
도 1은 본 발명의 고농도 질소폐수 처리공정도1 is a high concentration nitrogen wastewater treatment process diagram of the present invention
도 2는 상기 수처리공정을 수행하는 데 필요한 장치의 배치도2 is a layout view of an apparatus for performing the water treatment process;
<도면의 주요부분에 대한 부호의 설명><Description of the symbols for the main parts of the drawings>
1 : 단일 응집침전조2 : 간헐포기 SBR 반응조1: single flocculation settling tank 2: intermittent aeration SBR reactor
3 : 탈산소조4 : 연속식 여상 반응조(SMR)3: deoxygenation tank 4: continuous filter reactor (SMR)
5 : 침전조5: settling tank
본 발명은 질소부하가 높은 폐수를 처리함에 있어서 최근 발견된 반응식-1,2,3을 적용한다. 즉, SCOD가 적은 고농도의 질소폐수를 반응식-1,2에 따라 암모니아성 질소와 아질산성 질소의 비가 1:1.3이 되도록 전환하고, 반응식-3과 같은 혐기성 암모니아 산화반응에 의해 질소를 제거하는 공정이며, 도 2와 같이 단일 응집침전조(1)와 간헐포기 SBR 반응조(2), 탈산소조(3), 연속식 여상 반응조(4), 및 침전조(5)의 순으로 배치된 수처리장치에 의해 운용된다.The present invention applies the reaction schemes 1, 2, and 3 recently discovered in treating wastewater with high nitrogen load. That is, the process of converting high concentration nitrogen wastewater with less SCOD so that the ratio of ammonia nitrogen to nitrite nitrogen is 1: 1.3 according to Schemes 1 and 2, and removing nitrogen by anaerobic ammonia oxidation reaction as in Scheme-3 As shown in FIG. 2, a single flocculation sedimentation tank 1, an intermittent aeration SBR reactor 2, a deoxygenation tank 3, a continuous filter reactor 4, and a sedimentation tank 5 are operated in this order. do.
간헐포기 SBR 반응조(2)는 부분 아질산화와 유기물을 이용한 탈질을 반복하여 유기물의 농도가 적정수준 이하가 되는 시점에서 암모니아성 질소와 아질산성 질소의 비가 1:1.3이 되도록 부분 아질산화 반응을 수행하여 탈산소조로 보낸다.The intermittent aeration SBR reactor 2 repeats partial nitrite oxidation and denitrification using organic materials, and performs partial nitrous oxidation reaction so that the ratio of ammonia nitrogen and nitrite nitrogen is 1: 1.3 when the concentration of organic matter is below an appropriate level. To the deoxygenation tank.
탈산소조(3)는 혐기성 암모니아 산화공정의 방해인자인 산소를 제거하여 연속식 여상 반응조(4)로 보내고 침전 슬러지는 폐기한다. 연속식 여상 반응조(4)는 증식속도가 느린 혐기성 암모니아 산화균이 여재에 충분히 부착하여 성장할 수 있도록 고정상과 유동상 접촉여재를 교대로 설치하여 반응식-3과 같은 기작이 순조롭게 일어나도록 한다.The deoxygenation tank 3 removes oxygen, which is a blocker of the anaerobic ammonia oxidation process, and sends it to the continuous filter reactor 4 to dispose of the settling sludge. Continuous filter reactor (4) is a fixed bed and fluidized bed contact medium is installed alternately so that anaerobic ammonia oxidizing bacteria slow growth rate is attached to the filter medium sufficiently to grow mechanisms such as the scheme-3 occurs smoothly.
반응식-1 (부분아질산화반응)Scheme-1 (partial nitrous oxidation reaction)
{2 NH}`_{4 } ^{+ } +{3O}_{2 } ~→~ 2 { NO}`_{2 } ^{- } +4 { H}^{ +} +2 { H}_{2 } O (호기성){2 NH} `_ {4} ^ {+} + {3O} _ {2} ~ → ~ 2 {NO}` _ {2} ^ {-} +4 {H} ^ {+} +2 {H } _ {2} O (aerobic)
반응식-2 (탈질반응)Scheme-2 (Denitrification)
{2NO}`_{2 } ^{- } + { CH}_{3 } OH+ { CO}_{2 } ~→~ { N}_{2 } + { 2HCO}`_{3 } ^{- } + { H}_{2 } (무산소){2NO} `_ {2} ^ {-} + {CH} _ {3} OH + {CO} _ {2} ~ → ~ {N} _ {2} + {2HCO}` _ {3} ^ {- } + {H} _ {2} (oxic)
반응식-3 (혐기성 암모니아 산화반응)Scheme-3 (anaerobic ammonia oxidation)
{ 1NH}`_{4 } ^{+ } + { 1.31NO}`_{2 } ^{- } + { 0.0425CO}_{ 2} ~ →{1NH} `_ {4} ^ {+} + {1.31NO}` _ {2} ^ {-} + {0.0425CO} _ {2} ~ →
{ 1.045N}_{2 } + { 0.22NO}`_{3} ^{- } +1.87 { H}_{2 } O+ { 0.09OH}^{- } + {0.0425CH }_{2 } O(혐기성){1.045N} _ {2} + {0.22NO} `_ {3} ^ {-} +1.87 {H} _ {2} O + {0.09OH} ^ {-} + {0.0425CH} _ {2} O (Anaerobic)
각 반응조의 역할은 다음과 같다. 먼저, 단일 응집침전조(1)에서는 유입수가 간헐포기 SBR 반응조(2)로 유입되기에 앞서 혐기성 암모니아 산화반응의 방해인자인 인과 유기물을 응집제를 사용하여 화학적으로 침전시켜 제거한다. 여기서 90%에 달하는 인과 75%정도의 유기물이 제거되도록 한다.The role of each reactor is as follows. First, in a single flocculation sedimentation tank (1), before the inflow of water enters the intermittent aeration SBR reactor (2), phosphorus and organic substances, which are obstacles to the anaerobic ammonia oxidation reaction, are chemically precipitated and removed using a flocculant. Here, 90% of phosphorus and 75% of organic matter are removed.
또, 간헐포기 SBR 반응조(2)는 상기한 반응식-1(부분 아질산화반응)과 반응식-2(탈질반응)가 교대로 일어나도록 간헐포기를 하여 유기물을 소모한 후 재포기하여(반응식-1) 암모니아성 질소와 아질산성 질소의 비가 1:1.3이 되도록 한다. 이 간헐포기 SBR 반응조(1)는 나이트로조모나스(Nitrosomonas sp.)의 증식속도를 빠르게 하여 질산화 반응을 억제하고 아질산화 반응을 유도하기 위해 온도를 30∼35℃로 유지하고 미생물 체류시간(SRT)은 1.0∼3.0일이 되도록 운영한다.In addition, the intermittent aeration SBR reactor (2) was intermittently aerated so that the reaction formula-1 (partial nitrous oxidation reaction) and the reaction formula-2 (denitrification reaction) described above alternately consume the organic matter and then re-aeration (Scheme-1) ) The ratio of ammonia nitrogen to nitrite nitrogen is 1: 1.3. The intermittent aeration SBR reactor 1 maintains the temperature at 30-35 ° C. and maintains the microbial residence time (SRT) in order to speed up the growth rate of nitrosomonas sp. ) Runs for 1.0 to 3.0 days.
그리고 간헐포기 SBR 반응조(2)의 운전조건은 다음과 같다. 유입수는 상기한 바와 같이 단일 응집침전조(1)에서 인과 유기물이 제거되며, pH는 포기에 의해 CO2가 탈기되며 탈질시 알칼리도가 보충되므로 알칼리도의 추가적 주입 없이 7∼8로 유지된다. 또, 열교환기를 이용하여 수온을 30∼35℃로 유지하고, SCOD/NO2 --N의 비가 2가 되는 시점까지 포기한 후 무산소 상태에서 유기물을 이용하여 탈질함으로써 유기물을 소모하도록 간헐포기를 한다.And the operating conditions of the intermittent aeration SBR reactor 2 are as follows. As mentioned above, phosphorus and organics are removed in a single coagulation settling tank 1, and pH is maintained at 7 to 8 without additional injection of alkalinity since CO 2 is degassed by aeration and replenishment of alkalinity. In addition, maintaining the temperature by using a heat exchanger to 30~35 ℃ and, SCOD / NO 2 - -N ratio after giving up to the point of where the second, using an organic material in an oxygen-free state, the intermittent giving to consume organic material by denitrification.
또한 상기한 간헐포기과정을 통하여 유기물의 농도가 적정수준 이하가 된 후 암모니아성 질소와 아질산성 질소의 비가 1:1.3이 될 때까지 재포기하며 유출시에는 슬러지를 침전시키지 않고 교반상태에서 탈산소조(3)로 유출시켜 1.0∼3.0일의 짧은 SRT를 유지한다. 그리고 상기 공정은 복수계열로 설치해 운영함으로써 단일 응집침전조(1)에서 SBR 반응조(2)로의 연속유입이 이루어지록 한다.In addition, after the intermittent aeration process, the concentration of organic matter is lower than an appropriate level, and the air is reaerated until the ratio of ammonia nitrogen and nitrite nitrogen is 1: 1.3. Spill to (3) to maintain a short SRT of 1.0 to 3.0 days. In addition, the process is installed and operated in a plurality of series so that a continuous inflow from the single flocculation settling tank (1) to the SBR reaction tank (2).
탈산소조(3)는 혐기성 암모니아 산화반응의 방해인자인 산소를 제거하여 연속식 여상 반응조(4)로 보내고 침전된 슬러지는 폐기한다.The deoxygenation tank 3 removes oxygen, which is a blocker of the anaerobic ammonia oxidation reaction, and sends it to the continuous filter reactor 4 to discard the sludge deposited.
연속식 여상 반응조(4)는 하향류에서는 고정상 여재를 설치하여 혐기성 암모니아 산화균을 최대한 포집할 수 있도록 하고 상향류에서는 유동상 여재에 부착된 미생물이 질소폐수와 최대한 접촉하도록 하여 미생물이 최대한 부착하여 성장할 수 있도록 하며, 이를 교대로 설치하여 반응식-3과 같은 혐기성 암모니아 산화가 원활히 일어나도록 한다.The continuous filter reactor (4) has a fixed bed filter installed in the downflow to collect the anaerobic ammonia oxidizing bacteria as much as possible, and in the upstream, the microorganisms attached to the fluidized bed filter make the maximum contact with the nitrogen wastewater, so that the microorganisms can be It can be grown and alternately installed so that anaerobic ammonia oxidation smoothly occurs as in Scheme-3.
연속식 여상 반응조(4)의 운전조건은 혐기성 유지를 위해 유동상으로 가스를 재순환하고, 수리학적 체류시간(HRT)은 1.5∼2.0일, pH는 7∼8로 유지하며 온도는 열교환기를 이용하여 30∼35℃로 유지한다.Operation conditions of the continuous filter reactor (4) is to recycle the gas to the fluidized bed to maintain anaerobic, hydraulic retention time (HRT) of 1.5 to 2.0 days, pH of 7 to 8 to maintain the temperature using a heat exchanger Maintain at 30-35 degreeC.
침전조(5)는 침전된 슬러지의 90% 이상을 혐기성 암모니아 산화조(4)로 반송하고 상징액만 방류한다.The settling tank 5 returns more than 90% of the precipitated sludge to the anaerobic ammonia oxidation tank 4 and discharges only the supernatant.
이상 설명한대로 본 발명은 간헐포기 SBR 반응조와 탈산소조 및 연속식 여상 반응조를 이용하여 부분 아질산화와 혐기성 암모니아 산화반응을 일으키는 것으로 외부 탄소원의 공급 없이도 고농도 질소폐수를 아주 효과적으로 처리할 수 있다.As described above, the present invention generates partial nitrous oxidation and anaerobic ammonia oxidation by using an intermittent aeration SBR reactor, a deoxygenation tank, and a continuous filter reactor, so that a high concentration of nitrogen wastewater can be treated very effectively without supplying an external carbon source.
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